Process for cryogenic separation of a feed stream containing methane and air gases, facility for producing biomethane by purification of biogases derived from non-hazardous waste storage facilities (nhwsf) implementing the process

ABSTRACT

A process for cryogenic separation of a feed stream containing methane and air gases in which: the feed stream is cooled in order to produce a cooled stream, at least one portion of the cooled stream is sent to one level of a distillation column, a bottom stream is drawn off from the distillation column, the bottom stream being enriched in methane relative to the feed stream, a stream enriched in oxygen and in nitrogen relative to the feed stream is drawn off from the distillation column, at least one noncombustible dilution stream that is more volatile than oxygen is introduced into the distillation column at at least one level lower than the one at which the cooled stream is introduced. The dilution stream is extracted from the feed stream. Facility for producing biomethane by purification of biogases derived from non-hazardous waste storage facilities (NHWSF) implementing the process.

TECHNOLOGICAL FIELD

The present disclosure relates to a process and device for cryogenicseparation of a stream containing methane, carbon dioxide, nitrogenand/or oxygen and more generally air gases, for producing a methaneenriched stream.

The disclosed process has a particularly advantageous application inconnection with biomethane production by purification of biogas fromnonhazardous waste storage facilities (NHWSF).

BACKGROUND

Biogas is a gas produced by a biological process of breakdown of organicmatter in an anaerobic environment, that is primarily composed ofmethane, carbon dioxide, water vapor and impurities in variablequantities depending on the organic material having produced the biogas.The impurities that are mainly found are hydrogen sulfide and when theorganic material comes from household or industrial wastes, volatileorganic compounds (VOCs).

The biogas can be produced in dedicated reactors (also called“digesters”) where the biological reaction operates in a perfectlyanaerobic environment and with a controlled temperature. It can also beproduced naturally in significant quantities in nonhazardous wastestorage facilities (NHWSF), in which household wastes are stored invaults and covered with a membrane when they are full. After the vaultis closed, the process of methane production the organic material canbegan. The biogas thus produced is then collected by aspiration into abooster via collection tubes inserted in the vaults, thus creating aslightly reduced pressure in said vaults. Since these are not perfectlysealed, air is aspirated and found in the biogas in variable proportion.For this gas source, air gases therefore add to the previously mentionedimpurities and must be removed to recover the biogas.

There are also other sources of gas containing methane, carbon dioxide,impurities and a variable concentration of air gases, like gas frommines, produced by degassing of coal seams in abandoned mines, andmixing with air present in the mining spaces. With the goal ofrecovering this gas for the applications mentioned above, the impuritiesthat it contains must be eliminated.

More specifically, in order to produce a methane enriched stream, it isnecessary to remove the carbon dioxide, nitrogen and oxygen impuritiesto a level such that the methane enriched stream thus produced can beused as natural gas, liquefied natural gas or vehicle fuel. Depending onthe uses indicated, the required impurity level can vary. Just the same,a typical target for these impurities in the methane enriched stream is:under 2% by mole carbon dioxide, under 1% oxygen and under 1% nitrogen.When the methane enriched stream no longer contains carbon dioxide,required impurity level is: under 2.5% by mole nitrogen and under 1%oxygen.

The compositions in the remainder of the application are expressed inmolar percentages.

In the case of biogas produced by NHWSF, a first treatment is necessaryto remove most carbon dioxide and impurities. Many processes exist forthat, like the use of gas permeation membranes combined with thetreatment of impurities by adsorption (US-2004-0103782), the use ofpressure modulated adsorption processes, the use of washing columns withwater or amines and the use of cryotrapping processes. The biogasimpurities and the majority of the carbon dioxide can be knocked downwith these processes, but the air gases cannot be separated from themethane enriched gas stream. An additional treatment step is thereforerequired.

This additional treatment step can consist of pressure modulatedadsorption with the use of specific adsorbents selective for nitrogenand oxygen (U.S. Pat. No. 8,221,524). However, a very low oxygen andnitrogen concentration is achieved at the detriment of the methanerecovery rate from the process, which makes it economicallyuninteresting.

Another solution for removing air gases from methane is cryogenicdistillation which can achieve a good separation power between methaneon the one hand, recovered at the column bottom and oxygen and nitrogenon the other hand recovered at the column head, because of volatilitydifferences between these components.

However, the presence of oxygen, whose volatility is included betweenthat of methane and nitrogen, leads to this compound tending toconcentrate in the distillation zone and to do so even for small oxygenconcentrations in the column load. The increase of the gas phase oxygenconcentration added to the decrease of the gas phase methaneconcentration can lead to a gas mixture which is, because of thecomposition thereof, explosive.

The principle of distillation of the methane and air gases mixture is atcryogenic temperatures known, as is the appearance within the column ofpotentially explosive gas mixtures. Thus, the document DE 981,875proposes controlling the distillation in such a way that the gas leavingthe column head is outside the upper explosiveness limit (UEL). However,no mention is made of the natural oxygen concentration in thedistillation column and therefore the formation of an explosive gasmixture with this process cannot be avoided.

The document FR 1,410,494 identifies the risk of formation of thisexplosive mixture and proposes a means for avoiding the ignition of themixture by placing a metal foam between the levels the distillationcolumn with which to dissipate the methane oxidation reaction heat andtherefore avoid an explosion. However, the means proposed do not avoidthe methane oxidation reaction which will produce carbon dioxide andwater, these are undesirable compounds because they could block thecolumn at cryogenic temperatures.

The document U.S. Pat. No. 3,989,478 proposes to adjust the distillationsuch that the gas leaving the column head contains at least 20% methane,such that the composition of the gas phases in the distillation zone arenot explosive. The disadvantage of such an adjustment is both that ifthe column head gas contains 20% methane, and the remainder air, it isextremely close to explosiveness. Also, the loss of methane in the headgas is significant. Finally, no mention is made of the natural oxygenconcentration in the distillation column and therefore the formation ofan explosive gas mixture with this process cannot be avoided.

Another solution would be to dilute the gas and/or liquid mixtures fromthe distillation column such that this concentration is returned to avalue making the mixture nonexplosive in the areas having an enrichmentof the oxygen concentration.

Thus the document FR 2,971,331 proposes a dilution by pumping liquidmethane in the distillation column bottom and reinjection thereof in thecolumn head. Although the means proposed avoids formation of anexplosive mixture in the column, it leads to increasing the inventoriesof liquid methane in the column, and therefore the stored energy, whichis not desirable from the process safety perspective. Also a liquidmethane pump has to be installed which is a source of potentiallydangerous leaks.

The document FR 2,971,332 proposes avoiding the formation of anexplosive mixture within the column by dilution with nitrogen taken froman external source. It is therefore necessary to use a fluid, nitrogen,for the dilution. The fluid has a cost and therefore increases theoperating costs for the process. It should be noted that in thisdocument, the methane in the gas state injected in the column bottom isa combustible stream coming from the condenser-re-boiler. It is usedexclusively as a rising gas phase in connection with the distillation ofthe feed stream. Without such a stream, distillation is not possible.

The document U.S. Pat. No. 2,519,955 describes a production process fora methane and oxygen mixture. The idea is not to separate the methanefrom the oxygen to reduce the explosion risk but instead to combinethem. Essentially, the process consists of decompressing a biologicalgas stream rich in methane but depleted of oxygen and then to recoverthe heat produced within an exchanger placed in a distillation column.Within the exchanger, a portion of the feed stream composed of liquidmethane is reinjected in the column bottom whereas the other partcomposed of nitrogen is reinjected in the column head at a level higherthan that of the feed stream. The nitrogen stream is therefore not usedas dilution stream but serves to limit the loss of methane by occupyingthe column head volume.

Further, in order to be able to perform the separation of O₂ and N₂relative to CH₄ by cryogenic distillation, it is necessary to have astream whose CO₂ concentration is particularly low. The commonlyaccepted value is 50 ppmv—parts per million by volume—of carbon dioxidemaximum to avoid crystal formation which would plug the cryogenicexchangers. Similarly, water must be eliminated to avoid freezing.

To resolve that problem, the document FR 2,917,489 proposed regeneratingthe adsorbents used in the temperature or pressure modulated adsorbersby means of methane enriched gas, collected at the foot of thedistillation column in the liquid state and next vaporized. Thedisadvantage of the use of this fluid for regeneration resides in theneed to control the quantity of carbon dioxide to a constant value atthe outlet of the adsorbent bed, by mixing the bed outlet stream with amethane enriched stream. This control is made necessary because themethane enriched stream containing a small quantity of carbon dioxidecoming from the regeneration is intended to be used in biomethane form.However, in order to be injected in the natural gas network, it muststrictly satisfy the quality requirements of the network operator.

SUMMARY OF THE DISCLOSURE

The present disclosure addresses the problem of improving a process forcryogenic separation of the mixture for which the concentrations arealways outside the explosiveness zone and that does not have thedisadvantages raised above.

The present disclosure also addresses the problem of regenerating theadsorbents used in the temperature or pressure modulated adsorbers froma stream coming from the cryogenic separation without leading to theaforementioned drawbacks.

To resolve these problems and others, the Applicant developed acryogenic separation process in which the O₂ dilution stream consistsessentially of nitrogen and comes from the feed stream and not anexternal source. An obvious cost reduction results.

More precisely, the object of the present disclosure is a cryogenicseparation process for a feed stream containing methane and air gaseswherein:

-   -   the feed stream is cooled to produce a cooled stream;    -   at least a portion of the cooled stream is sent to a level of a        distillation column;    -   a bottom stream is drawn off from the distillation column, where        the bottom stream is enriched in methane compared to the feed        stream;    -   a stream enriched in oxygen and nitrogen compared to the feed        stream is drawn off from the distillation column;    -   at least one dilution stream that is incombustible and more        volatile than oxygen (meaning a stream containing essentially        nitrogen) is added to the distillation column at least one level        below the level at which the cooled stream is added.

The process characterized in that the dilution stream is extracted fromthe feed stream.

In a preferred embodiment:

-   -   the cooled stream is at least partially condensed;    -   the at least partially condensed cooled stream is then        decompressed;    -   the dilution stream is produced by separation of the gas        fraction produced at the outlet of the decompression.

In practice, the feed stream contains 60 to 97% methane, between 3 and50% nitrogen and oxygen and 3% or less carbon dioxide.

The Applicant showed that the prior decompression of the feed stream forthe distillation column in a round-bottom separator, and then injectionof the gas phase comprising essentially nitrogen, thus produced, in thelow part of the packing of the distillation column, meaning upstreamfrom the gas stream, would lead to a sufficient dilution of the gaseousoxygen, whose concentrations, because of this sweeping flow, aresufficiently low that the mixture with methane is not inflammable. Theliquid fraction of the feed stream comprising essentially liquid methaneis for its part next injected in the head of the column to be distilled.

Because of the separation of the gas phase from the liquid phase of thefeed stream and the reinjection of all or part of this gas phase, it isnot necessary to use gaseous nitrogen coming from an outside source assweeping fluid, such that the nitrogen consumption decreases.

Just the same, the use of a gas coming from the feed stream to betreated itself as a dilution stream, whether it comes from decompressingthe cooled stream or at the end of another treatment step thereof, doesnot exclude combining it with a dilution stream coming from an externalsource. The two dilution streams can be added to the distillation columnin the form of one single mixture or separately.

In practice, it is necessary to cool the column head to condense therising nitrogen rich gas in said column head and as necessary a portionof the gas coming from the feed stream from the separator.

In a first embodiment, the column head is cooled by cooling the feedstream coming from the decompression by mixing it with a refrigerantfluid. In other words, the refrigerant fluid stream is used as a coldsource for condensation of the column head gas and participates in theeffect of dilution of the oxygen in the distillation column by providingthe condensation of only a portion of the gas coming from thedecompression of the feed stream, the other part constituting thedilution stream.

The feed stream is cooled either before the separator by mixing saidstream with the refrigerant fluid or in the separator by adding arefrigerant fluid directly into the separator.

In a second embodiment, the column head is cooled by means of arefrigerant fluid that is added directly to the column head.

In practice, the refrigerant fluid is liquid nitrogen.

In a specific embodiment, the column contains several distillationsegments and the dilution feed is introduced between two segments.

In practice, the distillation segments are in the form of packing ordistillation plateau. In all cases, the distillation segments arearranged so that the liquid phase releases the most volatile compoundsthereof to the gas phase and the gas phase releases the least volatilecompounds thereof to the liquid phase.

As already stated, the process has a particularly advantageousapplication in connection with biomethane production by purification ofbiogas from NHWS.

In order to be able to perform the separation of O₂ and N₂ relative toCH₄ by cryogenic distillation, it is necessary to have a stream whoseCO₂ concentration is particularly low. The commonly accepted value is 50ppmv—parts per million by volume—of carbon dioxide maximum to avoidcrystal formation which would plug the cryogenic exchangers. Similarly,water must be eliminated for the same reason.

In other words, and, prior to the cryogenic separation, a feed stream isprovided that is rich in methane, contains nitrogen and oxygen, and hasa CO₂ concentration that was previously reduced.

To do that, the CO₂ concentration is reduced by adding the CO₂ rich feedstream into at least one purification unit, preferably by adsorption,for example pressure (PSA) or temperature (PTSA) modulated, loaded withadsorbent able to reversibly adsorb the majority of the CO₂.

This type of purifier is known to the person skilled in the art. Inpractice, for continuous operation at least two PSA or PTSA are used inparallel with one being in adsorption for eliminating the carbon dioxidewhile the other is in regeneration. Regeneration is done by lowering thepressure and by sweeping with the previously heated gas supplying theenergy required for desorption.

In a first embodiment, the adsorbents used in the adsorbers areregenerated by means of the oxygen and nitrogen-rich gas stream drawnfrom the column head. In practice, the methane depleted stream drawnfrom the column head contains between 60 and 100% nitrogen and oxygen.

It was in fact found that the column head gas, methane depleted, andalso containing nitrogen gas injected in the column, had a sufficientflow rate, because of the nitrogen injection, to perform the heating andcooling cycle of the adsorbent sieve, necessary for the carbon dioxidedesorption, to be done during the regeneration time. In this case, it isno longer necessary to use the methane stream withdrawn from the columnbottom to regenerate the adsorbents and therefore to maintain a constantcarbon dioxide concentration in the bed outlet stream. It is thuspossible to withdraw the methane enriched stream in liquid form and makeuse of it as liquefied natural gas.

In practice, the methane enriched stream at column bottom containsbetween 95 and 100% methane.

The CO₂ loaded gas coming from regeneration can then be used in twodifferent ways: either the loaded gases sent to a system for destructionby oxygen, or, if the methane concentration is sufficient, the loadedgases sent to a combustion system for electricity production(cogeneration micro-turbine or engine).

In a second embodiment, the adsorbents used in the adsorbers areregenerated by means of methane-rich gas drawn from the column bottom.

Another subject of the disclosure is a facility for producing biomethaneby purifying biogas from non-hazardous waste storage facilities (NHWSF)implementing the process described above and comprises successively:

-   -   a unit for purification of carbon dioxide by adsorption able to        deplete the feed stream of carbon dioxide;    -   a heat exchanger able to cool the CO₂ depleted stream;    -   a condenser-reboiler able to condense the CO₂ depleted stream by        heat exchange with the liquid drawn off the column bottom;    -   a means for decompression of the condensed stream;    -   a round bottom separator for the liquid and gas phases from the        condensed stream;    -   a distillation column;    -   a conduit able to transport the liquid phase from the        round-bottom separator to a level of a distillation column;    -   a conduit able to transport the gas phase (dilution stream) from        the round-bottom separator into the column at least one level        lower than the level at which the liquid phase is added;    -   means connected to a refrigerant fluid source for sending the        liquid nitrogen stream to the point for mixing with the feed        stream, or directly into the round-bottom separator.

The facility further comprises:

-   -   means for withdrawing a methane enriched liquid stream from the        bottom of the column for sending it into the condenser-reboiler        and producing a methane enriched gas stream;    -   means for returning the methane enriched gas stream to the        column bottom;    -   means for collecting the methane depleted gas stream from the        column head and sending it to the heat exchanger;    -   means for collecting the methane enriched gas stream from the        column bottom and sending it to the heat exchanger;    -   means for collecting the methane depleted stream reheated in the        exchanger, or the methane enriched stream reheated in the        exchanger, to the purification unit.

BRIEF DESCRIPTION OF THE DRAWINGS

The disclosed process and facility and resulting benefits will becomeclear from the following examples supported by the attached figures.

FIG. 1 shows the explosiveness diagram of a methane, oxygen and nitrogenmixture.

FIGS. 2 to 4 are diagrams of a cryogenic separation unit integrated intoa facility (partially shown) for production of biomethane bypurification of biogas coming from nonhazardous waste storage (NHWS).The drawings differ in the final use of the streams after cryogenicseparation.

DETAILED DESCRIPTION

The explosiveness diagram for a methane, oxygen and nitrogen mixture isshown in FIG. 1 . In this diagram, the explosiveness zone is grayed. Thecomposition of the gas phase over the entire height of the column isshown with a dashed line for the case where the round bottom separatoris not installed; the vapor phase then crosses into the explosivenesszone. In the scenario where a round bottom phase separator is installed,and where the gas phase produced is used to sweep the packing, then thegas phase rising in the column is not explosive.

For each of FIGS. 2 to 4 , a feed gas stream (1), at a pressure includedbetween 5 and 15 bar absolute, comprising between 60 and 97% methane,between 3 and 50% nitrogen and oxygen, and 3% or less carbon dioxide isadded into the unit for purification by adsorption (2), advantageously aPTSA, in order to lower the water and carbon dioxide concentration to avalue less than or equal to 50 ppmv.

The stream thus produced (3) is then cooled in a heat exchanger (4) byexchanging heat with the methane enriched liquid stream (20) and themethane depleted stream (23). The cooled stream (5) is sent into areboiler condenser (6) where it is cooled again by heat exchange withthe bottom liquid, so that the bottom liquid can boil and generatemethane-rich gas which will be used in the distillation, and also tocondense the feed stream.

The condensed stream (7) is then decompressed in a decompression member(8) to the operating pressure of the column (18), included between 1 and5 bar absolute.

According to FIGS. 2 and 3 , a liquid nitrogen stream (13) coming fromliquid nitrogen storage (12) is decompressed in a decompression member(14) and the decompressed stream (15) is mixed with the feed stream (9),at point 16, to next be introduced in a round bottom container forseparation of liquid and gas phases (11). In an embodiment not shown,the liquid nitrogen is injected directly in the round-bottom separator.

The embodiment differs from the one shown in FIG. 4 in that the liquidnitrogen is injected directly in the upper part of the distillationcolumn, by means, for example, of an injection nozzle (16).

For all embodiments, the liquid nitrogen rich liquid phase (19) comingfrom the round-bottom separator (11) is next added into the upper partof the distillation column (18). The gas phase (17) is added into thelower part of the packing of the distillation column (18) to constitutethe sweeping gas and participate in the distillation.

Distillation thus produces two streams: a methane enriched stream (20),bottom of the distillation column, and a methane depleted stream (23)that is rich in O₂ and N₂ at the head of the distillation column.

A fraction of the methane enriched liquid stream (20) is sent to theexchanger (4) to be vaporized and form a gaseous stream (22). Thisgaseous stream can be used in two ways.

As shown in FIG. 2 , this gaseous stream (22) is used as is. It is sentfor injection into the natural gas network via an injection station, orto a compression station to produce compressed natural gas, for use in avehicle natural gas, for example.

As shown in FIG. 3 , this gaseous stream (22) is used to regenerate thepurification unit (2) and form a methane enriched stream (26) containingcarbon dioxide coming from regeneration of the purification unit. Thestream (26) is next sent to a compression station to produce compressednatural gas, for use in a natural gas vehicle, for example.

In an embodiment not shown, the methane enriched stream (20) is drawnoff in a liquid form and used as liquefied natural gas.

For all embodiments, the other fraction of the methane enriched liquidstream in column bottom is sent to the reboiler condenser (6) to bevaporized. The gas stream thus created (21) is sent to the distillationcolumn to create the rising vapor participating in the distillation.

The gas stream (23) comprising oxygen, nitrogen and a methane fractionis then sent to the exchanger (4) to be reheated.

In the embodiment shown in FIG. 2 , the stream (24) leaving theexchanger is used to regenerate the purification unit (2) and producethe stream (25), which is then treated for burning the residual methanein an oxidizer.

If the methane concentration is over 25%, the stream (25) can be used ina cogeneration engine or micro-turbine in order to produce electricity.

In the embodiment shown in FIG. 3 , the stream (25) is sent directly tothe methane oxidation or usage systems mentioned above.

1-11. (canceled)
 12. A method for cryogenic separation in a distillationcolumn of a feed stream containing a mixture of methane and air gasescomprising nitrogen and oxygen, the distillation column comprising adistillation head at the upstream most portion of the distillationcolumn and an oppositely disposed distillation bottom, and one or moredistillation segments arranged between the distillation head and thedistillation bottom, the method comprising: flowing the feed streamthrough a heat exchanger to cool the feed stream thereby forming acooled feed stream; flowing the cooled feed stream into a reboilercondenser to further cool the feed stream by heat exchange therebycondensing the feed stream into a condensed stream; decompressing thecondensed stream to an operating pressure of the distillation columnthereby forming a decompressed stream; flowing the decompressed streaminto a separator wherein the decompressed stream is separated in agaseous phase and a liquid phase, wherein the cooled feed stream iscooled in the reboiler condenser such that upon separation in theseparator, nitrogen in the decompressed stream preferentially separatesinto the gaseous phase and methane preferentially separates into theliquid phase such that concentrations of nitrogen, methane, and oxygenin the gaseous phase result in a nonflammable mixture; flowing theliquid phase into the distillation head such that the liquid phase flowsdownstream through the one or more distillation segments fordistillation; flowing the gaseous phase into the distillation columndownstream at least one of the distillation segments, wherein thegaseous phase flows into the distillation column as a sweeping gas andparticipates in distillation by diluting a concentration of gaseousoxygen present in the distillation column to thereby maintain a mixtureof nitrogen, methane and oxygen within the distillation column that isnonflammable; drawing, after distillation, a methane-rich bottom liquidstream off of the bottom of the distillation column and amethane-depleted gaseous stream off the distillation column at thedistillation head, wherein the methane-rich bottom liquid stream isenriched in methane as compared to the feed stream; wherein: a portionof the methane-rich bottom liquid stream is flowed into the reboilercondenser to cool by heat exchange the cooled feed stream, and theportion of the methane-rich liquid bottom stream is vaporized in thereboiler condenser into a methane-rich gaseous phase that is flowed intothe distillation column downstream of a location at which the gaseousphase from the separator is flowed into the distillation column as thesweeping gas.
 13. The method of claim 12, further comprising mixing adecompressed liquid nitrogen stream with the decompressed stream beforethe decompressed stream is flowed into the separator.
 14. The method ofclaim 12, further comprising flowing a refrigerant fluid into thedistillation column to cool the distillation column.
 15. The method ofclaim 14, wherein the refrigerant fluid is flowed into the distillationhead.
 16. The method of claim 14, wherein the refrigerant fluid isliquid nitrogen.
 17. The method of claim 12, further comprising flowingthe feed stream through at least one purification unit before flowingthe feed stream through the heat exchanger, wherein the purificationunit is loaded with an adsorbent capable of reversibly adsorbing CO₂ tothereby reduce a CO₂ concentration of the feed stream.
 18. The method ofclaim 17, wherein the purification unit is a unit for purification byadsorption of PSA or PTSA and wherein the PSA or PTSA is regenerated byflowing the methane-depleted gaseous stream drawn off the distillationcolumn through the purification unit.
 19. The method of claim 12,wherein the distillation column comprises at least two distillationsegments, wherein the gaseous phase is flowed into the distillationcolumn between the adjacent ones of the at least two distillationsegments and the methane-rich gaseous phase from the reboiler condenseris flowed below both of the adjacent ones of the at least twodistillation segments.
 20. The method of claim 12, wherein the condensedstream is decompressed to a pressure between 1 and 5 bar absolute. 21.The method of claim 12, wherein the methane-depleted gaseous streamdrawn off of the distillation column at the distillation head is flowedinto the heat exchange to cool the feed stream by heat exchange.
 22. Themethod of claim 12, wherein the method is free of a flow of gaseousnitrogen into the distillation column from an external source fordilution of oxygen within the distillation column.
 23. A facility forproducing biomethane by purifying biogas from non-hazardous wastestorage facilities (NHWSF) implementing the method according to claim 12and comprising successively: the heat exchanger for cooling the feedstream; the reboiler condenser for condensing the cooled feed stream byheat exchange with the methane-rich bottom liquid stream drawn off thedistillation column; a decondenser for decondensing the condensedstream; the separator, wherein the separator is a round-bottom separatorfor separating the decompressed stream into the liquid and gas phases;the distillation column; a conduit for transporting the liquid phasefrom the round-bottom separator into the distillation head of thedistillation column; a conduit for transporting the gaseous phase fromthe separator into the distillation column; and a conduit forwithdrawing the methane enriched stream from the bottom of thedistillation column.
 24. The facility of claim 23, further comprising apurification unit upstream of the heat exchanger for reducing aconcentration of CO₂ in the feed stream.
 25. The facility of claim 23,further comprising a refrigerant fluid storage unit and a conduit forflowing the refrigerant fluid into the distillation column and/or into aconduit for mixing with the decondensed stream prior to introduction ofthe decondensed stream into the separator.